A polypropylene resin comprising a propylene polymer endowed with the following characteristics: a) distribution of molecular weight mw/Mn lower than 4; b) the melt-viscosity measured at a temperature of 250° C. in the shear rate range between 1000 1/s and 40000 1/s meet the following relationship: c) h 9*e(−0.00006*sr)+2 a. wherein h represents the melt-viscosity in Pas and sr the shear rate in 1/s d) the isotactic pentads (mmmm) measured with by 13C-NMR are higher than 90%; d) preferably higher than 92%; more preferably higher than 95% and most preferred higher than 96%; e) the hexane extractables according fda regulations are preferably below 2.6 wt. %; and f) the xylene solubles are below 2 wt. %; with the proviso that the propylene polymer was not visbroken.
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1. A polypropylene resin comprising a propylene polymer, the propylene polymer comprising:
a distribution of molecular weight mw/Mn lower than 43;
a melt-viscosity measured at a temperature of 250° C. in a shear rate ranging from 1000 1/s to 40000 1/s, and the melt-viscosity satisfies the following relationship:
h≦9*e(−0.00006*sr)+2 wherein
h is the melt-viscosity in Pas; and
sr is the shear rate in 1/s;
isotactic pentads (mmmm) measured with 13C-NMR are higher than 90%;
a hexane extractables according fda regulations are below 2.6 wt. %; and
xylene solubles are below 2 wt. %;
with the proviso that the propylene polymer was not visbroken.
13. A hygienic fabric comprising a polypropylene resin, the polypropylene resin comprising a propylene polymer, the propylene polymer comprising:
a distribution of molecular weight mw/Mn lower than 3;
a melt-viscosity measured at a temperature of 250° C. in a shear rate ranging from 1000 1/s to 40000 1/s, and the melt-viscosity satisfies the following relationship:
h≦9*e(−0.00006*sr)+2 wherein
h is the melt-viscosity in Pas; and
sr is the shear rate in 1/s;
isotactic pentads (mmmm) measured with 13C-NMR are higher than 90%;
a hexane extractables according fda regulations are below 2.6 wt. %; and
xylene solubles are below 2 wt. %;
with the proviso that the propylene polymer was not visbroken.
14. A filtration tool comprising a polypropylene resin, the polypropylene resin comprising a propylene polymer, the propylene polymer comprising:
a distribution of molecular weight mw/Mn lower than 3;
a melt-viscosity measured at a temperature of 250° C. in a shear rate ranging from 1000 1/s to 40000 1/s, and the melt-viscosity satisfies the following relationship:
h≦9*e(−0.00006*sr)+2 wherein
h is the melt-viscosity in Pas; and
sr is the shear rate in 1/s;
isotactic pentads (mmmm) measured with 13C-NMR are higher than 90%;
a hexane extractables according fda regulations are below 2.6 wt. %; and
xylene solubles are below 2 wt. %;
with the proviso that the propylene polymer was not visbroken.
2. The polypropylene resin according to
3. The polypropylene resin according to
4. The polypropylene resin according to
5. The polypropylene resin according to
6. The polypropylene resin according to
h≦7.25*e(−0.00006*sr)+2 wherein
h is the melt-viscosity in Pas; and
sr is the shear rate in 1/s.
7. The polypropylene resin according to
8. The polypropylene resin according to
9. The polypropylene resin according to
10. The polypropylene resin according to
11. The polypropylene resin according to
12. The polypropylene resin according to
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The present invention relates to a propylene polymer having high Melt flow rate and low extractables.
Propylene polymers have been used for years for obtaining films and molded articles. When used for particular applications such as food packaging and medical tools the value of extractables with solvents is an important parameter in order to evaluate the quality of the material. Two important parameters to be considered are the hexanes extractables according FDA regulations, and xylene solubles at 25° C. From another point of view propylene polymers having high melt flow rate have the drawback to have generally higher value of extractables. Due to process restrictions the polymerization of products with conventional Ziegler/Natta catalysts, high melt flow rates are limited to values of about 400 g/10′. To increase the melt flow rate further, the addition of peroxides is required. Despite the cost disadvantage for the peroxide, additional decomposition residuals from the peroxide have to be considered.
U.S. Pat. No. 5,741,563 relates to shrink films obtained by using a propylene polymers having a melt flow rate from 0.5 to 30 dg/min and hexane extractables are preferably less than 1% by weight.
Thus it would be desirable for certain applications to have propylene polymers endowed with low level of extractables and at the same time high melt flow rate values without any residuals coming from peroxidic or other kinds of degradation. In fact it is well known in the art that when a polymer is degradated with peroxides or other similar method, such as gamma rays some properties of the polymer becomes worse such as the yellowing index.
Thus the object of the present invention is a polypropylene resin comprising a propylene polymer endowed with the following characteristics:
The process for visbreaking a polymer consists in increasing the MFR of the latter by lowering the molecular weight of the polymers by means of chemical reactions such as radical reaction initiated by peroxides. The polymers obtained in this way presents some drawback, such as an high yellowing index, for this reason the polypropylene resin object of the present invention does not contains residues of peroxidic compounds.
Preferably the propylene polymer of the present invention has a melting point measured by means of DSC higher than 145° C.; preferably higher than 148° C., more preferably higher than 150° C., even more preferably higher than 153° C.
Preferably the propylene polymer of the present invention has a melt-viscosity at 250° C. according the general formula h≦K*e(−L*sr)+M in the shear rate range from 1000 1/s til 40000 1/s and more preferred in the shear rate range 2000 1/s til 30000 1/s.
in a preferred composition the values of the constants are given by K=9, L=0.00006 and M=2, more preferred K=7.25, L=0.00006 and M=2 and even more preferred K=2.5, L=0.00006 and M=2. Most preferred are the values K=2.5, L=0.00006 and M=1.3.
Preferably the melt-viscosity at a temperature of 250° C. and a shear rate of 1000 1/s is ≧1 Pas.
The propylene polymer of the present invention has preferably a content of 2,1-insertions lower than 0.5%, more preferred ≦0.3%. measured by 13C NMR spectroscopy as described below. The content of 1,3 insertions is preferably below 0.2%, more preferred ≦0.1%, it is measured by 13C NMR spectroscopy as described below.
The propylene polymer of the polypropylene resin object of the present invention is a propylene homopolymer.
The polypropylene resin of the present invention preferably further comprises customary amounts of customary additives known to those skilled in the art, e.g. stabilizers, lubricants and mold release agents, fillers, nucleating agents, antistatics, plasticizers, dyes, pigments, anti-fungal, anti-microbial agents, film cavitating agents or flame retardants. In general, these are incorporated during granulation of the powdery product obtained in the polymerization or the powder will be directly coated with the additives.
Customary stabilizers include antioxidants such as sterically hindered phenols, sterically hindered amines or UV stabilizers, processing stabilizers such as phosphites or phosphonites, acid scavengers such as calcium stearate or zinc stearate or dihydrotalcite, as well as calcium, zinc and sodium caprylate salts. In general, the propylene copolymer compositions of the present invention contain one or more stabilizers in amounts of up to 2% by weight.
Suitable lubricants and mold release agents are, for example, fatty acids, calcium, sodium or zinc salts of fatty acids, fatty acid amides or low molecular weight polyolefin waxes, which are usually used in concentrations of up to 2% by weight.
Possible fillers are, for example, talc, calcium carbonate, chalk or glass fibers, and these are usually used in amounts of up to 50% by weight.
Examples of suitable nucleating agents are inorganic additives such as talc, silica or kaolin, salts of monocarboxylic or polycarboxylic acids, e.g. sodium benzoate or aluminum tert-butylbenzoate, dibenzylidenesorbitol or its C1-C8-alkyl-substituted derivatives such as methyldibenzylidenesorbitol, ethyldibenzylidenesorbitol or dimethyldibenzylidenesorbitol or salts of diesters of phosphoric acid, e.g. sodium 2,2′-methylenebis(4,6,-di-tert-butylphenyl)phosphate. The nucleating agent content of the propylene copolymer composition is generally up to 5% by weight.
Such additives are generally commercially available and are described, for example, in Gächter/Müller, Plastics Additives Handbook, 4th Edition, Hansa Publishers, Munich, 1993.
In a preferred embodiment, the propylene polymer compositions of the present invention contain a 1:1 mixture of sterically hindered phenols and phosphites or phosphonites. The content of this mixtures ranges from 0.03% to 1% by weight, preferably from 0.05 to 0.2500% by weight and more preferred from 0.1 to 0.2% by weight (tradename of such products are Irganox B 501W from Ciba Specialty Chemical).
The polypropylene resin object of the present invention can be used in many applications, such as in compounding as masterbatchses and melt blown applications, for example hygienic fabrics and filtration applications.
The propylene polymer of the polypropylene resin object of the present invention can be obtained by using a metallocene-based catalyst system.
In particular said propylene polymer is obtainable by using a catalyst system obtainable by contacting:
##STR00001##
Preferably the substituent R1 is a linear C1-C20-alkyl radical such as methyl or ethyl radicals and the substituent R5 is a branched C1-C20-alkyl radical, preferably the substituent R5 is a branched C1-C20-alkyl radical wherein the carbon atom in the alpha position is a secondary or a tertiary carbon atom, such as an isopropyl radical.
Alumoxanes used as component b) in the catalyst system according to the present invention can be obtained by reacting water with an organo-aluminium compound of formula HjAlU3-j or HjAl2U6-j, where the U substituents, same or different, are hydrogen atoms, halogen atoms, C1-C20-alkyl, C3-C20-cycloalkyl, C6-C20-aryl, C7-C20-alkylaryl or C7-C20-arylalkyl radicals, optionally containing silicon or germanium atoms, with the proviso that at least one U is different from halogen, and j ranges from 0 to 1, being also a non-integer number. In this reaction the molar ratio of Al/water is preferably comprised between 1:1 and 100:1.
The alumoxanes used in the process according to the invention are considered to be linear, branched or cyclic compounds containing at least one group of the type:
##STR00002##
wherein the substituents U, same or different, are defined above.
In particular, alumoxanes of the formula:
##STR00003##
can be used in the case of linear compounds, wherein n1 is 0 or an integer of from 1 to 40 and the substituents U are defined as above; or alumoxanes of the formula:
##STR00004##
can be used in the case of cyclic compounds, wherein n is an integer from 2 to 40 and the U substituents are defined as above.
Examples of alumoxanes suitable for use according to the present invention are methylalumoxane (MAO), tetra-(isobutyl)alumoxane (TIBAO), tetra-(2,4,4-trimethyl-pentyl)alumoxane (TIOAO), tetra-(2,3-dimethylbutyl)alumoxane (TDMBAO) and tetra-(2,3,3-trimethylbutyl)alumoxane (TTMBAO).
Particularly interesting cocatalysts are those described in WO 99/21899 and in WO01/21674 in which the alkyl and aryl groups have specific branched patterns.
Non-limiting examples of aluminium compounds that can be reacted with water to give suitable alumoxanes (b), described in WO 99/21899 and WO01/21674, are:
Among the above aluminium compounds, trimethylaluminium (TMA), triisobutylaluminium (TIBA), tris(2,4,4-trimethyl-pentyl)aluminium (TIOA), tris(2,3-dimethylbutyl)aluminium (TDMBA) and tris(2,3,3-trimethylbutyl)aluminium (TTMBA) are preferred.
Non-limiting examples of compounds able to form an alkylmetallocene cation are compounds of formula D+E−, wherein D+ is a Brønsted acid, able to donate a proton and to react irreversibly with a substituent X of the metallocene of formula (I) and E− is a compatible anion, which is able to stabilize the active catalytic species originating from the reaction of the two compounds, and which is sufficiently labile to be removed by an olefinic monomer. Preferably, the anion E− comprises one or more boron atoms. More preferably, the anion E− is an anion of the formula BAr4(−), wherein the substituents Ar which can be identical or different are aryl radicals such as phenyl, pentafluorophenyl or bis(trifluoromethyl)phenyl. Tetrakis-pentafluorophenyl borate is particularly preferred compound, as described in WO 91/02012. Moreover, compounds of formula BAr3 can be conveniently used. Compounds of this type are described, for example, in the International patent application WO 92/00333. Other examples of compounds able to form an alkylmetallocene cation are compounds of formula BAr3P wherein P is a substituted or unsubstituted pyrrol radical. These compounds are described in WO01/62764. Compounds containing boron atoms can be conveniently supported according to the description of DE-A-19962814 and DE-A-19962910. All these compounds containing boron atoms can be used in a molar ratio between boron and the metal of the metallocene comprised between about 1:1 and about 10:1; preferably 1:1 and 2.1; more preferably about 1:1.
Non limiting examples of compounds of formula D+E− are:
Additional examples of compounds of formula D+E− that can be used according to the present invention are described in WO 04/005360, WO 02/102811 and WO 01/62764.
Organic aluminum compounds used as compound c) are those of formula HjAlU3-j or HjAl2U6-j as described above.
The catalysts described above can also be supported on an inert carrier. This is achieved by depositing the metallocene compound a) or the product of the reaction thereof with the component b), or the component b) and then the metallocene compound a) on an inert support such as, for example, silica, alumina, Al—Si, Al—Mg mixed oxides, magnesium halides, styrene/divinylbenzene copolymers, polyethylene or polypropylene. The supportation process is carried out in an inert solvent such as hydrocarbon for example toluene, hexane, pentane or propane and at a temperature ranging from 0° C. to 100° C., preferably the process is carried out at room temperature.
A suitable class of supports which can be used is that constituted by porous organic supports functionalized with groups having active hydrogen atoms. Particularly suitable are those in which the organic support is a partially crosslinked styrene polymer. Supports of this type are described in European application EP-633 272.
Another class of inert supports particularly suitable for use according to the invention is that of polyolefin porous prepolymers, particularly polyethylene.
A further suitable class of inert supports for use according to the invention is that of porous magnesium halides such as those described in International application WO 95/32995.
The solid compound thus obtained, in combination with the further addition of the alkylaluminium compound either as such or prereacted with water if necessary, can be usefully employed in the gas-phase polymerization.
The following examples are given for illustrative purpose and do not intend to limit the invention.
All data was obtained according to the following methods:
Rheological Measurements/Melt-Viscosity:
Determined according ISO 11443. Measurements were performed with a Goettfert Rheograph 2002 Capillary Rheometer at 3 different temperatures (200° C., 230° C. and 250° C.). Capillary length/diameter ratio was 40 (length 20 mm, diameter 0.5 mm). Entrance angle 180°
Following abbreviations were used:
Molecular weights and molecular weight distribution were measured at 145° C. using a Alliance GPCV 2000 instrument (Waters) equipped with three mixed-bed columns TosoHaas TSK GMHXL-HT having a particle size of 13 μm. The dimensions of the columns were 300×7.8 mm. The mobile phase used was vacuum distilled 1,2,4-Trichlorobenzene (TCB) and the flow rate was kept at 1.0 ml/min. The sample solution was prepared by heating the sample under stirring at 145° C. in TCB for two hours. The concentration was 1 mg/ml. To prevent degradation, 0.1 g/l of 2,6-diterbutyl-p-cresol were added. 326.5 μL of solution were injected into the column set. A calibration curve was obtained using 10 polystyrene standard samples (EasiCal kit by Polymer Laboratories) with molecular weights in the range from 580 to 7500000; additionally two other standards with peak molecular weight of 11600000 and 13200000 from the same manufacturer were included. It was assumed that the K values of the Mark-Houwink relationship were:
A third order polynomial fit was used for interpolate the experimental data and obtain the calibration curve. Data acquisition and processing was done by using Empower 1.0 with GPCV option by Waters.
Intrinsic Viscosity:
Intrinsic viscosity was measured in tetrahydronaphtalene (THN) solution obtained by dissolving the polymer at 135° C. for 1 hour.
FDA Extractables
Code of Federal Regulations, Title 21, Volume 3, Revised as of Apr. 1, 2004, CITE: 21CFR177.1520
Xylene-Soluble Faction
2.5 g of polymer and 250 mL of o-xylene are introduced in a glass flask equipped with a refrigerator and a magnetical stirrer. The temperature is raised in 30 minutes up to the boiling point of the solvent. The so obtained solution is then kept under reflux and stirring for further 30 minutes. The closed flask is then kept for 30 minutes in a bath of ice and water and in thermostatic water bath at 25° C. for 30 minutes as well. The solid thus obtained is filtered on quick filtering paper and 100 ml of the filtered liquid is poured in a previously weighed aluminum container, which is heated on a heating plate under nitrogen flow, to remove the solvent by evaporation. The container is then kept on an oven at 80° C. under vacuum until constant weight is obtained. The residue is weighted to determine the percentage of xylene-soluble polymer.
Melt Flow Rate (MFR)
Determined according to ISO 1133 (230° C., 2.16 Kg).
The ISO norm describes the procedure of measuring the MFR values til 150 g/10′. To measure the MFR value of products with higher MFR (up to ca. 3000 g/10′) the unmodified procedure was applied.
Melting temperature, melting enthalpy (ΔHm), crystallization temperature and crystallization enthalpy (ΔHc) determined by DSC according ISO 3146 with a heating rate of 20K per minute
13C-NMR
The assignments of PP spectra were made according to “Selectivity in Propylene Polymerization with Metallocene Catalysts”, L. Resconi, L. Cavallo, A. Fait, F. Piemontesi, Chem. Rev., 100, 1253, (2000))
The mmmm content was obtained modelling the experimental pentad distribution with the enantiomorphic site model. The mmmm content of PP with high content of 2,1 (E) and 1,3 (H) errors was obtained as:
The content of 2,1 and 3,1 errors was obtained as:
The catalyst system is prepared as described in PCT/EP2004/007061 by using rac-dimethylsilylene(2-methyl-4(4′tertbutyl-phenyl)-indenyl) (2-isopropyl-4(4′tertbutyl-phenyl)-indenyl)zirconium dichloride prepared as described in US 2003/0149199 instead of rac-dimethylsilylbis(2-methyl-4,5-benzo-indenyl)-zirconium dichloride.
Propylene Polymerization
The catalyst system in the form of catalyst mud obtained as described in PCT/EP2004/007061 is fed in the precontact vessel in which it is diluted with about 5 (Kg/h) of propane. From the pre-contact vessel the catalyst system is fed to the prepolymerization loop in which propylene is fed at the same time according to the data reported in table 1. The residence time of the catalyst in the prepolymerization loop is 8 minutes. The prepolymerized catalyst obtained in the prepolymerization loop is then continuously feed into the first loop reactor in which propylene, is fed according to table 1. The polymer is discharged from the first loop reactor, separated from the unreacted monomer and dried. The reaction conditions are reported in table 1. The MFR of the product is controlled by the feed of hydrogen.
TABLE 1
Prepolymerization
C3
H2
temperature
Ex
temperature (° C.)
(Kg/h)
(ppm (mol))
(° C.)
1
45
328
525
70
2
45
333
738
70
3
45
339
900
70
The isotactic pentades (mmmm) of all samples were higher than 95% (measured 96.4%) (13C-NMR). The 2.1 insertions are ≦0.3% and the 1.3 insertions are ≦0.1% (13C-NMR).
The products were characterized according table 2. The tests themselves were carried out in accordance with the standards indicated in table 2.
TABLE 2
Exam-
Exam-
Exam-
Method
Variable Name
Units
ple 1
ple 2
ple 3
ISO1133
Melt Flow Rate
g/10 min
605
1335
1700
ISO3146
Hc
J/g
−97.6
−97.4
−96.9
ISO3146
Hm
J/g
95.8
96.9
−96.7
ISO3146
Tm
deg_C.
155
156
153
ISO3146
Tc
deg_C.
104.2
104.6
104.2
Intrinsic
dl/g
0.62
0.54
<0.5
viscosity
Xylene solubles
%
0.6
0.8
1
Mn (GPC)
g/mol
n.m.
43497
39883
Mw(GPC)
g/mol
n.m.
89997
86864
Mw/Mn
2.1
2.1
2.2
FDA
Hexane
%
0.4
0.4
0.7
Extractables
100 u film
The melt-viscosity was determined according ISO 11443 at three different temperatures (200° C.; 230° C. and 250° C.). The results are reported in tables 3—
TABLE 3
Example 1
Shear
Shear
viscosity
Melt-
rate
Melt-
200° C.
viscosity
230° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
g (s−1)
tapp (Pa)
h (Pa*s)
89979.4
167776.0
1.9
69256.5
137244.0
2.0
37067.2
132358.0
3.6
32244.4
103505.0
3.2
16005.3
99688.6
6.2
14904.6
73430.6
4.9
7246.6
70682.7
9.8
6963.1
48699.3
7.0
3410.9
46867.4
13.7
3320.5
30227.2
9.1
1656.3
29463.8
17.8
1607.8
17403.5
10.8
806.3
16640.2
20.6
784.5
9312.4
11.9
397.1
9007.1
22.7
195.2
4579.9
23.5
96.4
2289.9
23.8
48.8
1068.6
21.9
Shear
rate
Melt-viscosity
250° C.
h
g (s−1)
tapp (Pa)
h (Pa*s)
9 *e (−0.00006* sr) + 2
71027.8
121672.0
1.7
2.126889
30983.3
88849.5
2.9
3.402458
14144.1
60149.0
4.3
5.851946
6738.6
38928.9
5.8
8.006899
3275.4
23510.0
7.2
9.394235
1597.0
12976.3
8.1
10.17765
775.8
6564.5
8.5
10.59067
TABLE 4
Example 2
Shear
Shear
rate
Melt-
rate
Melt-
200° C.
viscosity
230° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
g (s−1)
tapp (Pa)
h (Pa*s)
52354.8
134496.0
2.6
51466.7
108085.0
2.1
24755.7
99077.9
4.0
26745.7
75415.2
2.8
12873.9
68850.8
5.3
13614.5
49310.0
3.6
6747.0
45035.4
6.7
6750.4
30074.5
4.5
3457.4
27173.9
7.9
3274.4
16945.5
5.2
1725.2
15113.6
8.8
1578.4
8701.8
5.5
844.9
7938.5
9.4
770.2
4274.6
5.6
408.1
3969.2
9.7
391.2
1984.6
5.1
193.5
1832.0
9.5
Shear
rate
Melt-
250° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
9 *e (−0.00006* sr) + 2
57794.5
91750.1
1.6
2.280707
27355.4
61065.0
2.2
3.74351
13183.5
38318.3
2.9
6.08048
6482.0
22594.0
3.5
8.100096
3210.7
12365.7
3.9
9.422995
1572.6
6106.5
3.9
10.18963
774.0
2747.9
3.6
10.5916
398.4
1221.3
3.1
10.78741
TABLE 5
Example 3
Shear
Shear
rate
Melt-
rate
Melt-
200° C.
viscosity
230° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
g (s−1)
tapp (Pa)
h (Pa*s)
60486.3
107474.0
1.8
61014.7
79842.5
1.3
28397.9
75567.9
2.7
27915.6
53126.5
1.9
13685.5
50989.3
3.7
13188.7
32364.4
2.5
6661.9
31143.1
4.7
6729.8
18777.5
3.0
3079.6
13587.0
5.1
3174.0
10533.7
3.3
1544.0
5190.5
3.4
Shear
rate
Melt-
250° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
9 *e (−0.00006* sr) + 2
49759.5
67171.5
1.3
2.454596
25828.9
43356.1
1.6
3.91074
13150.1
25952.6
2.0
6.088665
6582.1
14655.6
2.2
8.063569
3254.6
7938.5
2.4
9.403468
1574.8
3969.2
2.5
10.18855
Comparative example 4 was polymerized according Example 1-3 with the polymerization conditions reported in table 6.
TABLE 6
Comp.
Prepolymerization
C3
H2
temperature
Ex 4
temperature (° C.)
(Kg/h)
(ppm (mol))
(° C.)
4
45
328
480
70
Characterization of comparative sample 4 gave the following results:
TABLE 7
Comparative
Method
Variable Name
Units
Example 4
ISO1133
Melt Flow Rate
g/10 min
390
ISO3146
Hc
J/g
−94.9
ISO3146
Hm
J/g
93.3
ISO3146
Tm
° C.
154
ISO3146
Tc
° C.
104.9
Intrinsic viscosity
dl/g
0.69
Xylene solubles
%
<0.5
Mn (GPC)
g/mol
n.m.
Mw(GPC)
g/mol
n.m.
Mw/Mn
n.m.
FDA
Hexane Extractables, 100 u
%
0.4
film
The rheological characterization gave the following results:
TABLE 8
Comparative Example 4
Shear
Shear
rate
Melt-
rate
Melt-
200° C.
viscosity
230° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
g (s−1)
tapp (Pa)
h (Pa*s)
89022.4
187011.0
2.1
85533.9
155868.0
1.8
38689.5
150525.0
3.9
35799.8
121519.0
3.4
17103.6
117855.0
6.9
15655.5
90223.5
5.8
7704.6
86864.9
11.3
7171.8
63507.6
8.9
3584.2
60912.3
17.0
3393.7
41524.2
12.2
1705.1
39692.2
23.3
1640.9
25189.3
15.4
824.0
23968.0
29.1
806.9
14502.9
18.0
401.4
13434.3
33.5
395.3
7633.1
19.3
197.1
7175.1
36.4
193.7
3816.6
19.7
96.9
3663.9
37.8
96.9
1832.0
18.9
48.0
1832.0
38.2
Shear
rate
Melt-
250° C.
viscosity
g (s−1)
tapp (Pa)
h (Pa*s)
9 *e (−0.00006* sr) + 2
76149.7
139686.0
1.8
2.093317
32309.1
103810.0
3.2
3.295217
14548.0
73125.3
5.0
5.75972
6838.5
48394.0
7.1
7.971001
3296.5
29769.2
9.0
9.384879
1615.6
17250.9
10.7
10.16853
790.5
9159.8
11.6
10.5831
383.6
4427.2
11.5
10.79522
Fuchs, Alexander, Bugada, Daniele, Emrich, Janine
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